CN207047125U - A kind of system that aromatic hydrocarbons is prepared by coal with flue gas reuse function - Google Patents
A kind of system that aromatic hydrocarbons is prepared by coal with flue gas reuse function Download PDFInfo
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- CN207047125U CN207047125U CN201720798552.0U CN201720798552U CN207047125U CN 207047125 U CN207047125 U CN 207047125U CN 201720798552 U CN201720798552 U CN 201720798552U CN 207047125 U CN207047125 U CN 207047125U
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- 239000003245 coal Substances 0.000 title claims abstract description 79
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 72
- 239000003546 flue gas Substances 0.000 title claims abstract description 25
- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 24
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 claims abstract description 140
- -1 acetylene aromatic hydrocarbons Chemical class 0.000 claims abstract description 77
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 claims abstract description 64
- 239000005997 Calcium carbide Substances 0.000 claims abstract description 57
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 claims abstract description 57
- 238000004140 cleaning Methods 0.000 claims abstract description 36
- 239000000463 material Substances 0.000 claims abstract description 28
- 238000006243 chemical reaction Methods 0.000 claims description 112
- 239000007789 gas Substances 0.000 claims description 98
- 239000000571 coke Substances 0.000 claims description 91
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 50
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 50
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 46
- 239000001257 hydrogen Substances 0.000 claims description 41
- 229910052739 hydrogen Inorganic materials 0.000 claims description 41
- 238000002485 combustion reaction Methods 0.000 claims description 35
- 238000010438 heat treatment Methods 0.000 claims description 35
- 230000008676 import Effects 0.000 claims description 31
- 235000019738 Limestone Nutrition 0.000 claims description 28
- 239000001569 carbon dioxide Substances 0.000 claims description 25
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 25
- 239000006028 limestone Substances 0.000 claims description 25
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 24
- 239000000919 ceramic Substances 0.000 claims description 21
- 239000007787 solid Substances 0.000 claims description 20
- 150000002431 hydrogen Chemical class 0.000 claims description 17
- 238000007599 discharging Methods 0.000 claims description 16
- 239000002737 fuel gas Substances 0.000 claims description 16
- 229930195733 hydrocarbon Natural products 0.000 claims description 15
- 150000002430 hydrocarbons Chemical class 0.000 claims description 15
- 238000000746 purification Methods 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 11
- 238000011049 filling Methods 0.000 claims description 10
- 239000004215 Carbon black (E152) Substances 0.000 claims description 7
- 238000004519 manufacturing process Methods 0.000 abstract description 19
- 238000000034 method Methods 0.000 abstract description 17
- 230000008569 process Effects 0.000 abstract description 5
- 125000003118 aryl group Chemical group 0.000 abstract description 3
- 239000003208 petroleum Substances 0.000 abstract description 3
- 230000007704 transition Effects 0.000 abstract description 2
- 238000006555 catalytic reaction Methods 0.000 description 36
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 24
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 24
- 229910052799 carbon Inorganic materials 0.000 description 24
- 238000000197 pyrolysis Methods 0.000 description 19
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 18
- 238000001816 cooling Methods 0.000 description 16
- 238000002156 mixing Methods 0.000 description 16
- 239000000047 product Substances 0.000 description 13
- 239000000292 calcium oxide Substances 0.000 description 12
- 235000012255 calcium oxide Nutrition 0.000 description 12
- 230000004044 response Effects 0.000 description 12
- 239000012495 reaction gas Substances 0.000 description 11
- 239000002245 particle Substances 0.000 description 9
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 8
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 8
- 150000001875 compounds Chemical class 0.000 description 8
- 238000010304 firing Methods 0.000 description 8
- 230000008439 repair process Effects 0.000 description 8
- 239000003863 metallic catalyst Substances 0.000 description 7
- 229910001220 stainless steel Inorganic materials 0.000 description 7
- 239000010935 stainless steel Substances 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- 239000011280 coal tar Substances 0.000 description 6
- 238000010924 continuous production Methods 0.000 description 6
- 229910052751 metal Inorganic materials 0.000 description 6
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- 230000009719 regenerative response Effects 0.000 description 5
- 239000004575 stone Substances 0.000 description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 4
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 4
- 230000003197 catalytic effect Effects 0.000 description 4
- 229910052750 molybdenum Inorganic materials 0.000 description 4
- 239000011733 molybdenum Substances 0.000 description 4
- 229910052759 nickel Inorganic materials 0.000 description 4
- 229910052763 palladium Inorganic materials 0.000 description 4
- 229910052703 rhodium Inorganic materials 0.000 description 4
- 239000010948 rhodium Substances 0.000 description 4
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 3
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 3
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- 230000031068 symbiosis, encompassing mutualism through parasitism Effects 0.000 description 3
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
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- 238000005265 energy consumption Methods 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
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- 241001120493 Arene Species 0.000 description 1
- 241000790917 Dioxys <bee> Species 0.000 description 1
- FDTGUDJKAXJXLL-UHFFFAOYSA-N acetylene Chemical group C#C.C#C FDTGUDJKAXJXLL-UHFFFAOYSA-N 0.000 description 1
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Abstract
A kind of system that aromatic hydrocarbons is prepared by coal with flue gas reuse function is the utility model is related to, the system includes material pretreatment system, cleaning system, furnace of calcium carbide, acetylene generator and acetylene aromatic hydrocarbons reactor.The utility model is solved the problems, such as the aromatic production limitation brought because petroleum resources are limited, is realized the transition process of the aromatic hydrocarbons from the low-order coal of low value to high added value by coal aromatic hydrocarbons.
Description
Technical field
The group technology that light aromatics is prepared by coal is the utility model is related to, more particularly, to a kind of low-order coal and stone
Lime stone production acetylene, hydrogen etc., then the system by acetylene production light aromatics.
Background technology
The energy general layout in China is always rich coal, oil-poor, few gas, coal reserves up to world's coal reserves 17%.Its
The low-order coal resource reserve such as middle lignite, jet coal enriches, and accounts for coal in China reserves and coal production more than 50%, but due to low order
Coal water content is high, directly burns or gasification efficiency is low and prior art can not make full use of its resource value, result in coal money
The huge waste in source.In April, 2015, National Energy Board issued《Coal Clean efficiently utilizes action plan (2015-2020)》,
Coal sub-prime classified utilization status is significantly improved, vigorously advocates the research and development and demonstration of low-order coal upgrading technology.Therefore, develop low
The clean and effective of rank coal has very great display meaning using new way.
The light aromatics such as benzene, toluene and dimethylbenzene are one of most important Elementary Chemical Industry raw material, are widely used in producing rubber
The chemical products such as glue, fiber, plastics and dyestuff.At present, aromatic hydrocarbons is mainly derived from catalytic reforming and hydro carbons heat in petrochemical industry
Solution, only about 10% derives from coal chemical industry.But petroleum resources are more and more deficienter at present, therefore, develop new by low-order coal
The technology for producing the light aromatics such as benzene is imperative.
The method for utilizing dry distillation of coal product preparing light aromatics from coal tar in the prior art, this method cut into coal tar
<200 DEG C of light fractions and>200 DEG C of heavy ends, light fraction enter two fixed bed hydrogenation reactors and carry out selective add
Hydrogen, the product of gained obtain the light aromatics such as benzene,toluene,xylene through processes such as air lift, distillation, solvent extractions.This method is used
Coal tar substitutes oil and produces light aromatics, is the favourable supplement of aromatics production.But the coal tar oil yield obtained by the dry distillation of coal compared with
It is low, generally less than 5%, and in coal tar<200 DEG C of cuts are less than 30%, and light components content is lower in high temperature coal-tar, therefore
It is less that this method produces light aromatics yield, does not make full use of coal resources to produce aromatic hydrocarbons, it is impossible to fundamentally to solve stone
The aromatic production that oily scarcity of resources is brought reduces problem.
Therefore, in order to overcome technological deficiency of the prior art, it is necessary to which a kind of produce the light aromatics such as benzene by low-order coal
Technology.
Utility model content
In view of the above-mentioned problems, the purpose of this utility model is to provide a kind of system that light aromatics is prepared by coal.
To reach above-mentioned purpose, the utility model adopts the following technical scheme that：
A kind of system that aromatic hydrocarbons is prepared by coal with flue gas reuse function, comprising：
Material pretreatment system, there are multiple entrance and exits, for coal and lime stone to be pyrolyzed and fired respectively,
First gas and the first solid, and second gas and the second solid are obtained,
Cleaning system, including the first cleaning system, the first cleaning system have first gas material inlet and multiple outlets,
For first gas material purification separation to be obtained into hydrogen, methane, carbon monoxide and light hydrocarbon gas；
Furnace of calcium carbide, the furnace of calcium carbide have the first import, first outlet and CO gas outlet, and the first of furnace of calcium carbide enters
Mouth is used to be sent into the first solid and the second solid；The CO gas of furnace of calcium carbide is exported for discharging carbon monoxide；
Acetylene generator, the acetylene generator have the second import and a second outlet, the second import of acetylene generator with
The first outlet of furnace of calcium carbide is connected；The second outlet of acetylene generator, which is used to discharge, contains acetylene gas；
Acetylene aromatic hydrocarbons reactor, the acetylene aromatic hydrocarbons reactor have feeding line, gas distributor, reaction sleeve pipe,
Heating furnace and discharging pipeline；Feeding line is provided with entrance and exit, and entrance is used to be passed through the hydrogen isolated from cleaning system
With methane, from the carbon monoxide of furnace of calcium carbide discharge and from acetylene made from acetylene generator；Gas distributor is arranged on reaction
The inside of sleeve pipe and positioned at reaction sleeve pipe upper end and with the outlet of feeding line；React filling ceramic honeycomb in sleeve pipe
Body；Reaction sleeve pipe runs through heating furnace, and heating furnace face reacts the middle part of sleeve pipe；Discharging pipeline connects with reacting the lower end of sleeve pipe.
Further, material pretreatment system includes：First coke oven and the second coke oven, the first coke oven are used to carry out heat to coal
Solution, the second coke oven are used to be fired lime stone；First coke oven has first material import, the first solid outlet and first
Gas vent, the second coke oven have second material import, the second solid outlet and second gas outlet；First coke oven and second
Coke oven is combustion chamber shared, and combustion chamber has fuel gas inlet and exhanst gas outlet.
Further, furnace of calcium carbide CO gas exit set flow divider, flow divider have the first diffluence pass and
Second diffluence pass, for CO gas to be divided into two-way, wherein all the way with the feeding line of acetylene aromatic hydrocarbons reactor
Entrance can breakaway-element connection, be connected all the way with the fuel gas inlet of combustion chamber in addition.
Further, the exhanst gas outlet of combustion chamber can breakaway-element company with the entrance of the feeding line of acetylene aromatic hydrocarbons reactor
Connect.
Further, cleaning system also includes the second cleaning system, the second cleaning system and the second gas of the second coke oven
Outlet is connected for purifying second gas, has second gas entrance and carbon dioxide outlet.
On the other hand, the method that light aromatics is prepared using above-mentioned system, is comprised the following steps：
1) low-order coal and lime stone enter material pretreatment system, respectively obtain upgraded coal and pyrolysis gas and quick lime and
Carbonated firing tail gas；
2) pyrolysis gas purifies by the first cleaning system, obtains hydrogen, methane, carbon monoxide and light aromatics；
3) by the quick lime obtained in step 1) and upgraded coal, hot charging, which enters in furnace of calcium carbide, fires production calcium carbide and an oxidation
Carbon；
4) calcium carbide for obtaining step 3), react with water to obtain acetylene in acetylene generator；
5) hydrogen obtained in step 2) and methane, step 3) are obtained into carbon monoxide and acetylene that step 4) obtains as
Reactor, which is passed through in acetylene aromatic hydrocarbons reactor, carries out thermal response and catalytic reaction, produces light aromatics, and by-product heavy arene
And ethene.
Further, make low-order coal be pyrolyzed to obtain upgraded coal and pyrolysis gas into the first coke oven, enter lime stone
Second coke oven is fired to obtain quick lime and carbonated firing tail gas, burnt to the first coke oven and second by combustion chamber
Stove heat.
Further, the carbon monoxide that step 3) obtains is split valve and is divided into two parts, and a part is passed through acetylene aromatic hydrocarbons
It is used to produce light aromatics in reactor, the carbon monoxide and light hydrocarbons blending transportation obtained in another part and step 2) is extremely
Combustion chamber, the fuel gas as burning.
Further, when the course of reaction of step 5) carries out a period of time, and has carbon deposit in reactor, method is also wrapped
Include：Recycling step 1) in the flue gas discharged of combustion chamber, close and be passed through the reaction gas of acetylene aromatic hydrocarbons reactor, be passed through flue gas, make
Flue gas reacts and generates hydrogen and carbon monoxide at high temperature with the carbon deposit in reactor, to make reactor again except carbon deposition removal
It is raw.
Further, method also includes：Carbonated firing tail gas is purified by the second cleaning system and obtains dioxy
Change carbon, and reaction gas of the carbon dioxide as aromatic hydrocarbons processed is passed through in acetylene aromatic hydrocarbons reactor.
" can breakaway-element connection " refers to that on-fixed connects in the utility model, and this connected mode refers to, it is necessary to when connecting
It can connect, it is necessary to can also be disconnected when disconnecting.
According to specific embodiment of the present utility model, there is provided a kind of system that light aromatics is prepared by coal, comprising：
First coke oven and the second coke oven, the first coke oven are used to coal is pyrolyzed and fired, and the second coke oven is used for lime
Stone is pyrolyzed and fired；First coke oven and the second coke oven have first material import and second material import, first solid respectively
Body exports and the second solid outlet and first gas outlet and second gas outlet；First coke oven and the second coke oven share burning
Room, combustion chamber have fuel gas inlet and exhanst gas outlet；
Mixing tank, the mixing tank have a compound import and compound outlet, and the compound import of mixing tank is respectively with the
First solid outlet of one coke oven and the second solid outlet of the second coke oven are connected；
First cleaning system, first cleaning system are connected for purification separation coal with the first gas outlet of the first coke oven
Obtained pyrolysis gas is pyrolyzed, the first cleaning system has pyrolysis gas import and multiple outlets, multiple to export for after discharge separation
Hydrogen, methane, carbon monoxide and light hydrocarbon gas；
Second cleaning system, second cleaning system are connected for purifying lime stone with the second gas outlet of the second coke oven
Obtained firing tail gas is fired, has and fires gas inlet and carbon dioxide outlet；
Furnace of calcium carbide, the furnace of calcium carbide have the first import, first outlet and CO gas outlet, and the first of furnace of calcium carbide enters
Mouth is connected with the compound outlet of mixing tank；The CO gas of furnace of calcium carbide is exported for discharging carbon monoxide；
Acetylene generator, the acetylene generator have the second import and a second outlet, the second import of acetylene generator with
The first outlet of furnace of calcium carbide is connected；The second outlet of acetylene generator, which is used to discharge, contains acetylene gas；
Acetylene aromatic hydrocarbons reactor, the acetylene aromatic hydrocarbons reactor have feeding line, gas distributor, reaction sleeve pipe,
Heating furnace and discharging pipeline；Feeding line is provided with entrance and exit, and entrance is used to be passed through what is isolated from the first cleaning system
Hydrogen and methane, the carbon dioxide obtained from the second cleaning system, occur from the carbon monoxide of furnace of calcium carbide discharge and from acetylene
Acetylene made from device；Gas distributor is arranged on the inside of reaction sleeve pipe and positioned at the upper end of reaction sleeve pipe and and feeding line
Outlet；React filling ceramic honeycomb body in sleeve pipe；Reaction sleeve pipe runs through heating furnace, and heating furnace face is reacted in sleeve pipe
Portion；Discharging pipeline connects with reacting the lower end of sleeve pipe；
Piece-rate system, the piece-rate system are connected with the discharging pipeline of acetylene aromatic hydrocarbons reactor and for separating acetylene system virtue
The product of hydrocarbon reactor.
Further, the system also includes：First disintegrator and the second pulverizer, first disintegrator and the second pulverizer point
It is not connected with the first material import of the first coke oven and the second material import of the second coke oven.
Further, furnace of calcium carbide CO gas exit set flow divider, flow divider have the first diffluence pass and
Second diffluence pass, the first diffluence pass of flow divider are used for the oxidation of entrance conveying one of the feeding line to acetylene aromatic hydrocarbons reactor
Carbon, the second diffluence pass of flow divider are connected with the fuel gas inlet of combustion chamber.
Further, the entrance of the feeding line of the exhanst gas outlet of combustion chamber and acetylene aromatic hydrocarbons reactor is can breakaway-element
Connection.
Further, the internal diameter of the reaction sleeve pipe of acetylene aromatic hydrocarbons reactor, the length of reaction sleeve pipe and the length of heating furnace
The ratio of degree is (2-10)：70：40.Here, react the internal diameter of sleeve pipe, react the ratio of the length of sleeve pipe and the length of heating furnace
Preferably 1：14：8.In the utility model, react the internal diameter of sleeve pipe, react the ratio of the length of sleeve pipe and the length of heating furnace
Determine, and after reaction temperature determines, heating furnace determines that to reacting the temperature field in sleeve pipe during reaction sleeve pipe heating
.
Further, acetylene aromatic hydrocarbons reactor also includes the first potted component and the second potted component, the first sealing member
Part is arranged on feeding line and is arranged on discharging pipeline with reacting the connection of sleeve pipe with reacting the junction of sleeve pipe, the second potted component
Place.
Further, when heating furnace is to reaction sleeve pipe heating, react in sleeve pipe, drawn successively from top to bottom according to temperature field
It is divided into preheating zone, thermal reaction area, heat-accumulating area, catalytic reaction zone and cooling zone.
In the utility model, heating furnace is referred in the middle part of the heating furnace face reaction sleeve pipe of acetylene aromatic hydrocarbons reactor
The distance between the distance between the middle part of corresponding reaction sleeve pipe, reaction sleeve upper end lower end is identical.It is such to be provided with
Beneficial to the constant of holding reaction temperature.Heating furnace sets temperature controlling point in thermal reaction area center.
In the utility model, ceramic honeycomb body is filled with the reaction sleeve pipe of acetylene aromatic hydrocarbons reactor, reacts sleeve pipe
Interior filling ceramic honeycomb body is advantageous to keep the temperature in reaction sleeve pipe, because the thermal capacitance of ceramic honeycomb body is larger, accumulation of heat effect
It is good.
Further, it is characterised in that preheating zone, thermal reaction area, heat-accumulating area, the length ratio of catalytic reaction zone and cooling zone
Example is (20-40)：(8-12)：(8-12)：(1-3)：(18-20).Under above-mentioned length ratio, the temperature field in sleeve pipe is reacted
It is distributed the continuous production most beneficial for aromatic hydrocarbons.
Further, at least two coke ovens are combustion chamber shared.
Further, the stainless steel reaction sleeve pipe that sleeve pipe is lined ceramicses is reacted.Stainless steel sleeve pipe liner is using ceramics
Because acetylene contacts stainless steel at high temperature will occur a large amount of side reactions, lined ceramicses can avoid contact of the acetylene with stainless steel,
Prevent side reaction.
Additionally, it is provided a kind of method for preparing light aromatics using system as above, comprises the following steps：
1) lime stone is fired into the first coke oven, obtains quick lime and carbon dioxide；
2) low-order coal enters the pyrolysis upgrading of the second coke oven, obtains pyrolysis gas and upgraded coal, and pyrolysis gas is by the second purification
System purification, obtains hydrogen, methane, carbon monoxide and light aromatics；
3) after the upgraded coal obtained in the quick lime and step 2) that are obtained in step 1) is mixed in mixing tank, hot charging is entered
Enter and production calcium carbide and carbon monoxide are fired in furnace of calcium carbide；
4) after the calcium carbide cooling that obtains step 3) is broken, react with water to obtain acetylene in acetylene generator；
5) hydrogen obtained in the carbon dioxide obtained in step 1), step 2) and methane, step 3) are obtained into an oxidation
The acetylene that carbon and step 4) obtain, which is passed through in acetylene aromatic hydrocarbons reactor, carries out thermal response and catalytic reaction, produces light aromatics,
And by-product heavy arene and ethene；
6) after the course of reaction of step 5) terminates, the reaction gas for being passed through acetylene aromatic hydrocarbons reactor is closed, is made in combustion chamber
Flue gas be passed through acetylene aromatic hydrocarbons reactor and carry out regenerative process, flue gas and carbon deposit react generation hydrogen and carbon monoxide.
Further, lime stone enters crushing also including lime stone before the first coke oven is fired in step 1)；Step 2)
Middle low-order coal enters broken also including low-order coal before the second coke oven.
Further, carbon dioxide：Hydrogen：Methane：Carbon monoxide：Acetylene quality proportioning is：5.5-9.1:1:2.66:
0.43-2.78:2.37-3.95, preferably 9.1：1：2.66：0.43：3.95.
Further, the carbon monoxide that step 3) obtains is split valve and is divided into two parts, and a part is passed through acetylene aromatic hydrocarbons
It is used to produce light aromatics in reactor, another part mixes with the carbon monoxide and light hydrocarbons obtained in step 2) passes through pipe
Road is delivered to the combustion chamber of the first coke oven and the second coke oven, the fuel gas as burning.
Further, step 1) and 2) in lime stone and low-order coal when firing and be pyrolyzed in coke oven, to combustion chamber discharge
Flue gas reclaimed, flue gas is passed through in acetylene aromatic hydrocarbons reactor in step 6), under high temperature with carbon deposit react remove product
Charcoal.
Further, step 1) and 2) in coke oven it is combustion chamber shared, chamber temperature be 1000 DEG C.
Further, the pyrolysis gas in step 2) also obtains carbon monoxide and light hydrocarbon after gas purge system purifies
Class, carbon monoxide and light hydrocarbons are used as fuel gas by the second diffluence pass of pipeline to flow divider and are delivered to coke oven.
Further, the firing time of coal upgrading and lime stone is 12 hours in step 3), step 1) and 2) in use
The mass ratio of low-order coal and lime stone is (1:1)~(1:2).
Further, quick lime and upgraded coal hot charging enter in furnace of calcium carbide and produce calcium carbide in step 3), can effectively reduce electricity
The energy consumption of stone stove, improve the heat utilization efficiency of system process.The carbon monoxide part that step 3) obtains is as acetylene aromatic hydrocarbons
Reaction gas, another part can provide thermal source as fuel gas for the combustion chamber of coke oven or the heating furnace of acetylene aromatic hydrocarbons reactor.
Further, the agstone of step 1) is broken to below 45mm；Preferable particle size is 5~45mm.Lime stone fires institute
The carrier gas that obtained carbon dioxide can react as acetylene aromatic hydrocarbons, raw material of the obtained quick lime as production calcium carbide.
Further, the low-order coal of step 2) is crushed to below 25mm；Preferable particle size is 5~25mm.Low-order coal refers to
Volatile matter be more than 35% low-quality coal, volatile matter pyrolysis gained pyrolysis gas purification can obtain hydrogen, methane, carbon monoxide,
The combustible components such as light hydrocarbons, wherein methane and hydrogen can be as the raw materials of acetylene aromatic hydrocarbons reactor in step 5), and remaining can
A part of carbon monoxide that furnace of calcium carbide obtains in combustion gas body and step 3) can be the combustion chamber of the coke oven of step 1) and step 2)
Thermal source.
Further, the calcium carbide in step 4) is crushed to below 80mm, and preferable particle size is 50~80mm.
Further, in step 5), when heating furnace is to reaction sleeve pipe heating, gas distributor bottom root in sleeve pipe is reacted
Preheating zone, thermal reaction area, heat-accumulating area, catalytic reaction zone and cooling zone are in turn divided into according to temperature field, heat is carried out in thermal reaction area
Reaction, thermal response temperature are 850~1100 DEG C, preferably 880~920 DEG C, catalytic reaction are carried out in catalytic reaction zone, catalysis is anti-
The temperature answered is 350~600 DEG C.Catalytic reaction uses metallic catalyst, and metallic catalyst is one in nickel, molybdenum, palladium, ruthenium or rhodium
Kind is several, and metallic catalyst is supported on ceramic honeycomb body.
Further, the ceramic honeycomb body for reacting the catalytic reaction zone in sleeve pipe is loaded with metallic catalyst.
Further, metallic catalyst is the one or more in nickel, molybdenum, palladium, ruthenium or rhodium, preferably metal Ru.
Further, the mass percent of metallic catalyst is 0.1%-5%.
In the utility model, catalytic reaction zone by after ceramic honeycomb body carried metal integral catalyzer filling and
Into wherein the metal loaded is the one or more in nickel, molybdenum, palladium, ruthenium or rhodium.Catalytic reaction generation occurs in catalytic reaction zone
Product.
Further, flue gas caused by combustion chamber when reclaiming coke oven heating, the regeneration for acetylene aromatic hydrocarbons reactor
Cheng Zhong, when acetylene aromatic hydrocarbons reactor continuous production light aromatics for a period of time after, carbon deposit can be produced in reactor and blocks hole,
Carbon dioxide and water and high temperature carbon deposit haptoreaction generation carbon monoxide and hydrogen in flue gas, remove carbon deposition removal with this, make reaction
Device is regenerated, and continues the continuous production of light aromatics.
Regenerative response process is：Carbon dioxide and water are rich in high-temperature flue gas caused by combustion chamber (temperature reaches 1000 DEG C)
Steam, acetylene aromatic hydrocarbons reactor is passed through, in thermal reaction area, carbon dioxide steams with high temperature carbon deposit reaction generation carbon monoxide, water
Gas and high temperature carbon deposit reaction generation carbon monoxide and hydrogen；In catalytic reaction zone, the work of carbon monoxide and vapor in catalyst
Hydrogen and carbon dioxide are generated with lower reaction, can be realized after obtained Hydrogen Separation purification as the unstripped gas of acetylene aromatic hydrocarbons
Effective utilization of resource.
Metallic catalyst light aromatics, the and can such as catalyzing acetylene trimerization generation benzene can exist in the course of reaction of step 5)
Carbon monoxide and steam reforming hydrogen manufacturing obtained by thermal reaction area are catalyzed in regenerative response.The reactor has coupled thermal response and urged
Change reaction, improve conversion of alkyne and light aromatics yield, make use of thermal response waste heat, effectively improve heat utilization efficiency, simultaneously
On-line regeneration can be achieved, and by-product hydrogen uses for course of reaction.
To ensure the continuous production of aromatic hydrocarbons, can two acetylene aromatic hydrocarbons reactors in parallel, an acetylene aromatic hydrocarbons reactor
Carry out catalytic polymerization under acetylene high temperature；Another acetylene aromatic hydrocarbons reactor carries out regenerative response, mutually switching.
The beneficial effects of the utility model are：
By coal aromatic hydrocarbons, the aromatic production for solving the problems, such as to bring because petroleum resources are limited limits the utility model,
Realize the transition process of the aromatic hydrocarbons from the low-order coal of low value to high added value.
The unstripped gas that the utility model reacts low-order coal upgrading, gaseous product as fuel gas and acetylene aromatic hydrocarbons；Carry
Matter coal and quick lime production calcium carbide, prepare acetylene, the unstripped gas as acetylene aromatic hydrocarbons reactor；Gas fume of combustion chamber is as acetylene
The unstripped gas of aromatic hydrocarbons reactor regeneration processed, the comprehensive high-efficiency for realizing resource utilize.
The utility model is loaded using ceramic honeycomb body, ensures the uniformity of thermal field in reactor, while prevents that catalysis is anti-
Area's bed is answered to block, pressure drop increase.
Acetylene aromatic hydrocarbons reactor of the present utility model has coupled thermal response and catalytic reaction, improves light aromatics production
Rate.Simultaneously on-line regeneration is realized using the flue gas of combustion chamber.
Brief description of the drawings
Fig. 1 is the schematic diagram according to the system that light aromatics is prepared by coal of embodiment of the present utility model；
Fig. 2 is the schematic diagram according to the acetylene aromatic hydrocarbons reactor of embodiment of the present utility model；
Fig. 3 is the process chart that light aromatics is prepared by coal according to embodiment of the present utility model.Reference
1 first disintegrator, 2 second pulverizers, 3 first coke ovens, 4 second coke ovens, 5 mixing tanks, 6 furnaces of calcium carbide, 7 acetylene occur
Device, 8 acetylene aromatic hydrocarbons reactors, 82 reaction sleeve pipes, 83 heating furnaces, 84 first potted components, 85 second potted components, 86 gases
Distributor, 87 feeding lines, 88 discharging pipelines, 89 preheating zones, 810 thermal reaction areas, 811 heat-accumulating areas, 812 catalytic reaction zones, 813
Cooling zone, 9 piece-rate systems, 10 first cleaning systems, 11 second cleaning systems, the 3rd coke oven 12, the 4th coke oven 13.
Embodiment
In order that the purpose of this utility model, technical scheme and advantage are more clearly understood, below in conjunction with the accompanying drawings and implement
Example, the utility model is further elaborated.It should be appreciated that specific embodiment described herein is only explaining this
Utility model, it is not used to limit the utility model.
As shown in figure 1, the system that the utility model uses includes：First disintegrator 1, the second pulverizer 2, the first coke oven 3,
Second coke oven 4, mixing tank 5, furnace of calcium carbide 6, acetylene generator 7, acetylene aromatic hydrocarbons reactor 8, the purification of piece-rate system 9, first system
The cleaning system 11 of system 10 and second.
The pulverizer 2 of first disintegrator 1 and second respectively with the first material import of the first coke oven 3 and the second coke oven 4
Two material inlets are connected, for will enter the first coke oven 3 and the second coke oven 4 after crushing material.First coke oven 3 is used to carry out coal
Pyrolysis and firing, the second coke oven 4 are used to lime stone is pyrolyzed and fired；First coke oven 3 and the second coke oven 4 have the respectively
One material inlet and second material import, the first solid outlet and the second solid outlet and first gas outlet and second gas
Outlet；First coke oven 3 and the second coke oven 4 are disposed adjacent, the pulverizer 2 of first disintegrator 1 and second respectively with the first coke oven 3 and
The first material import of two coke ovens 4 is connected with second material import；First coke oven 3 and the second coke oven 4 are combustion chamber shared, can be effective
Reduce system energy consumption.Combustion chamber has fuel gas inlet and exhanst gas outlet.The charging of exhanst gas outlet and acetylene aromatic hydrocarbons reactor 8
The entrance of pipeline 87 is can breakaway-element connection.Flue gas is delivered to acetylene aromatic hydrocarbons reactor 8 and carries out regenerative response with carbon deposit, is made
Obtain carbon deposit to be consumed, acetylene aromatic hydrocarbons reactor 8 can recycle, it is not necessary to stop work and carry out carbon deposit cleaning.This paper's " can disconnect
The connected mode that can as needed close with connect that formula connection " can be known to the skilled person, such as add one
Individual valve.In the course of reaction of acetylene aromatic hydrocarbons reactor 8, close valve and cause flue gas to cannot be introduced into acetylene aromatic hydrocarbons reactor
8；In the regenerative process of acetylene aromatic hydrocarbons reactor 8, reaction gas is closed, valve is opened and make it that flue gas is anti-into acetylene aromatic hydrocarbons
Answer device 8.
In addition, in embodiment as shown in Figure 1, four coke ovens are shown, the first coke oven is used to coal is pyrolyzed and burnt
System, the second coke oven are used to lime stone is pyrolyzed and fired；3rd coke oven 12 and the 4th coke oven 13 can be according to actual conditions
Coal and lime stone are pyrolyzed and fired respectively., can be with always according to the needs (for example, it is desired to number of product) of actual conditions
It is disposed adjacent two, four, six, multiple coke ovens such as eight.
There is mixing tank 5 compound import and compound to export, the compound import of mixing tank 5 with respectively with the first coke oven
Second solid outlet of 3 the first solid outlet and the second coke oven 4 is connected.
First cleaning system 10 is connected the pyrolysis gas obtained for purification separation pyrolysis of coal with the first coke oven 3, the first purification
System 10 has pyrolysis gas import and a multiple outlets, multiple to export for discharging the hydrogen after separating, methane, carbon monoxide and light
Matter hydrocarbon gas.First cleaning system 10 can be used well known to a person skilled in the art cleaning system, can be by purification separation
Various gases afterwards are discharged by different outlets.
Second cleaning system 11 is connected the firing tail gas obtained for purifying lime stone to fire with the second coke oven 4, has and burns
Gas inlet and carbon dioxide outlet processed.
Furnace of calcium carbide 6 has the first import, first outlet and CO gas outlet, and the first import of furnace of calcium carbide 6 is with mixing
The compound outlet of batch can 5 is connected；The CO gas exit of furnace of calcium carbide 6 sets flow divider, and flow divider has first point
Head piece and the second diffluence pass, the entrance that the first diffluence pass of flow divider is used for the feeding line to acetylene aromatic hydrocarbons reactor 8 are defeated
Carbon monoxide is sent, the second diffluence pass of flow divider is connected with the fuel gas inlet of combustion chamber, for conveying fuel gas to combustion chamber,
To provide the heat being pyrolyzed for the first coke oven 3 and the second coke oven 4.
Acetylene generator 7 has the second import and second outlet, the second import of acetylene generator 7 and the first of furnace of calcium carbide
Outlet is connected, and the second outlet of acetylene generator 7 is used to discharge acetylene.Acetylene aromatic hydrocarbons reactor 8 have feeding line 87 with
And discharging pipeline 88, wherein feeding line 87 are provided with entrance and exit.The entrance of feeding line 87 is net from first for being passed through
Hydrogen and methane that change system 10 is isolated, the carbon dioxide obtained from the second cleaning system 11, the oxygen discharged from furnace of calcium carbide 6
Change carbon and from acetylene made from acetylene generator 7.
Piece-rate system 9, piece-rate system 9 are used for separation product, piece-rate system 9 and the discharge nozzle of acetylene aromatic hydrocarbons reactor 8
Line 88 is connected and is used for the product for separating acetylene aromatic hydrocarbons reactor 8.
In another embodiment, be the continuous production that ensures aromatic hydrocarbons, can two acetylene aromatic hydrocarbons reactors in parallel, respectively
Course of reaction and regenerative process are carried out, mutually switching, improve production efficiency.
As shown in Fig. 2 acetylene aromatic hydrocarbons reactor 8 also includes gas distributor 86, the first potted component 85, second seals
Element 86, reaction sleeve pipe 82 and heating furnace 83, gas distributor 86 are arranged on the inside of reaction sleeve pipe 82 and positioned at reaction sleeve pipes
82 upper end and with the outlet of feeding line 87；React filling ceramic honeycomb body in sleeve pipe 82；Reaction sleeve pipe 82 runs through
Heating furnace 83, the face of heating furnace 83 react the middle part of sleeve pipe 82；Discharging pipeline connects with reacting the lower end of sleeve pipe 82.First sealing
Element 85 is arranged on feeding line 87 and is arranged on discharging pipeline and reaction with reacting the junction of sleeve pipe 82, the second potted component 86
The junction of sleeve pipe 82.React filling ceramic honeycomb body in sleeve pipe 82.Be tod because reaction gas contacts stainless steel under the high temperature conditions
The a large amount of side reactions of generation, therefore, stainless steel reaction sleeve pipe 82 are the stainless steel reaction pipe of lined ceramicses, feeding line 87 and product
Discharging line temperature preferably control below 200 DEG C.
Wherein, the middle part of the face of heating furnace 83 reaction sleeve pipe 82 refers to the middle part of the corresponding reaction sleeve pipe 82 of heating furnace 83,
The distance between the distance between reaction sleeve pipe 82 upper end lower end is identical.It is such to be provided with beneficial to holding reaction temperature
It is constant, and heating furnace 83 sets temperature controlling point in the center of thermal reaction area 810.
Ceramic honeycomb body is filled with reaction sleeve pipe 82, filling ceramic honeycomb body is advantageous to keep reaction in reaction sleeve pipe 82
Temperature in sleeve pipe 82, because the thermal capacitance of ceramic honeycomb body is larger, accumulation of heat effect is good.
Preferably, the ratio of the length of the internal diameter of reaction sleeve pipe 82, length and heating furnace 83 is (2-10)：70：40.This
In, the ratio for reacting the length of the internal diameter of sleeve pipe, the length of reaction sleeve pipe and heating furnace is preferably 1：14：8.
Preferably, when heating furnace 83 heats to reaction sleeve pipe 82, drawn from top to bottom according to temperature field in reaction sleeve pipe 82
It is divided into preheating zone 89, thermal reaction area 810, heat-accumulating area 811, catalytic reaction zone 812 and cooling zone 813.
Wherein, preheating zone 89, thermal reaction area 810, heat-accumulating area 811, catalytic reaction zone 812 and cooling zone 813 are by ceramics
Honeycomb ceramics filling forms, and ceramic honeycomb body has higher heat storage capacity, can improve energy utilization efficiency, ensures gas in heat
Reaction zone 810 has uniform thermal field.Catalytic reaction zone 812 by after ceramic honeycomb body carried metal integral catalyzer filling and
Into the metal of load is the metals such as nickel, molybdenum, palladium, ruthenium or rhodium, and load capacity is 0.1%~5%, and catalytic reaction zone 812 is not set individually
Temperature controlling point, the reaction of acetylene aromatic hydrocarbons be exothermic reaction, be able to will be urged using the waste heat that be taken out of of gas of thermal reaction area 810
Agent is filled to the region that temperature is 350~600 DEG C.Catalytic reaction zone 812 can make full use of the waste heat of thermal reaction area 810,
And can improves conversion of alkyne by catalytic reaction, increases the yield of light aromatics, improves the matter of liquid product obtained by thermal response
Amount, further improve light aromatics yield.Flowing resistance is advantageously reduced as carrier using self-contained ceramic honeycomb body simultaneously
Power, beds caused by Catalyst packing density is excessive or carbon deposit is more are avoided to block.
In acetylene aromatic hydrocarbons reactor, react the internal diameter of sleeve pipe 82, react the length of sleeve pipe 82 and the length of heating furnace 83
The ratio-dependent of degree, and after reaction temperature determines, heating furnace 83 is reacted in sleeve pipe 82 when being heated to reaction sleeve pipe 82
Temperature field determine that.
Preferably, the length of preheating zone 89, thermal reaction area 810, heat-accumulating area 811, catalytic reaction zone 812 and cooling zone 813
Ratio is (20-40)：(8-12)：(8-12)：(1-3)：(18-20).Under this ratio, the temperature highest of thermal reaction area 810, in advance
Secondly, the temperature of catalytic reaction zone 812 is lower, and the temperature of cooling zone 813 is minimum for hot-zone 89 and heat-accumulating area 811.React the temperature in sleeve pipe
Spend continuous production of the field distribution most beneficial for aromatic hydrocarbons.
In addition, the method that light aromatics is prepared using above-mentioned acetylene aromatic hydrocarbons reactor, including：Reaction gas is entered in proportion
Row mixing, is passed through feeding line 87 to gas distributor 86；By the mixed gas of gas distributor 86 in the pre- of reaction sleeve pipe
Hot-zone 89 is warming up to the thermal response temperature of thermal reaction area 810 by less than 200 DEG C of initial temperature, keeps permanent in thermal reaction area 810
Thermal response occurs for temperature, and reaction temperature is 850~1100 DEG C, and the preferable temperature of thermal reaction area 810 is 880~920 DEG C, more preferably
900℃；Again by the heat-accumulating area 811 of reaction sleeve pipe, catalytic reaction temperature is reduced to from thermal response temperature in the product of heat-accumulating area 811
Degree, catalytic reaction zone 812 is reached, is contacted with catalyst, catalytic reaction system occurs under the conditions of being 350 DEG C -600 DEG C in reaction temperature
It is standby to obtain product light aromatics；Obtained final product is by the cooling zone 813 of reaction sleeve pipe, and in cooling zone 813, temperature reduces
To less than 200 DEG C, then entered by the pipeline that discharges in downstream unit (not shown).
In the above-mentioned methods, acetylene is main reaction gas in reaction gas；Hydrogen suppresses acetylene as partial reaction gas
And the undue condensation of aromatic hydrocarbons, reduce carbon deposit；Methane and carbon monoxide can reduce the formation of carbon deposit；Carbon dioxide as carrier gas,
Reduce the partial pressure of acetylene.
In the above-mentioned methods, reaction feed air speed is 2000~6000h-1, the length based on this determination reaction time.
As shown in figure 3, preparing the method for light aromatics using system as above, comprise the following steps：
1) lime stone is crushed to below 45mm by first disintegrator 1 is broken, is fired into the first coke oven 3, obtains giving birth to stone
Ash and carbon dioxide, enter acetylene aromatic hydrocarbons reactor after being purified by the first cleaning system 10；
2) low-order coal is crushed to below 25mm by the second pulverizer 2 is broken, into the upgrading of the second coke oven 4, is pyrolyzed
Gas and upgraded coal, pyrolysis gas pass through the second cleaning system 11, obtain hydrogen and methane；Pyrolysis gas purifies through the second cleaning system 11
Carbon monoxide and light hydrocarbons, the second diffluence pass that carbon monoxide and light hydrocarbons pass through pipeline to flow divider are also obtained afterwards
Combustion chamber is delivered to as fuel gas.
3) after the upgraded coal obtained in the quick lime obtained in step 1) and step (2) is mixed in mixing tank 5, hot charging
12 hours production calcium carbides and carbon monoxide are fired into furnace of calcium carbide 6；
4) the calcium carbide cooling that step 3) obtains is crushed to after below 80mm in acetylene generator 7 and reacted with water, gas
Acetylene is obtained after purified；
5) oxygen for obtaining the hydrogen obtained in the carbon dioxide obtained in step 1), step 2) and methane, step 3)
To change the acetylene that carbon and step 4) obtain and be mixed into acetylene aromatic hydrocarbons reactor 8 and is reacted, reaction temperature is 850 DEG C-
1100℃.By preheating zone 89, thermal reaction area 810, heat-accumulating area 811, catalytic reaction zone 812 and cooling zone 813 production lightweight virtue
Hydrocarbon, and by-product heavy arene and ethene.
6) after the course of reaction of step 5) terminates, the reaction gas for being passed through acetylene aromatic hydrocarbons reactor 8 is closed, is made in combustion chamber
Flue gas be passed through acetylene aromatic hydrocarbons reactor 8 and carry out regenerative process, flue gas and carbon deposit react generation hydrogen and carbon monoxide,
And a part of vapor of having more than needed.
Step 1) and 2) in the first and second coke ovens it is combustion chamber shared, the flue gas that combustion chamber obtains enters acetylene aromatic hydrocarbons
In reactor regenerative response is carried out with carbon deposit.
The carbon monoxide that step 3) obtains is split valve and is divided into two parts, and a part is passed through in acetylene aromatic hydrocarbons reactor 8
For producing light aromatics, another part mixes by pipeline extremely with the carbon monoxide and light hydrocarbons obtained in step 2)
The combustion chamber of first coke oven and the second coke oven, the fuel gas as burning.
Step 1) and 2) in the mass ratio of the low-order coal that uses and lime stone be (1:1)~(1:2).
Reaction in step 5) is catalytic reaction, the catalysis temperature in the catalytic reaction zone 812 of acetylene aromatic hydrocarbons reactor
Spend for 350~600 DEG C.
Preferably, carbon dioxide：Hydrogen：Methane：Carbon monoxide：Acetylene quality proportioning is：5.5-9.1:1:2.66:
0.43-2.78:2.37-3.95, preferably 9.1：1：2.66：0.43：3.95.
When catalytic reaction uses ruthenium catalyst, ruthenium catalyst can in the course of reaction of step 5) catalyzing acetylene trimerization
The light aromatics such as benzene are generated, and can is catalyzed the carbon monoxide and steam transforming system of the gained of thermal reaction area 810 in regenerative process
Hydrogen.The reactor has coupled thermal response and catalytic reaction, improves conversion of alkyne and light aromatics yield, make use of thermal response
Waste heat, heat utilization efficiency is effectively improved, while on-line regeneration can be realized, and by-product hydrogen uses for course of reaction.
Embodiment 1
As Figure 1-3, agstone is broken to below 45mm, from 5~45mm particle diameters, through belt-conveying to first Jiao
Stove 3 is fired.Middle low-order coal is crushed to below 25mm, from 5~25mm particle diameters, is pyrolyzed through belt-conveying to the second coke oven 4.It is low
Rank coal is 1 with lime stone mass ratio:2, the combustion chamber heating-up temperature of coke oven is 1000 DEG C.After 12h is fired and is pyrolyzed, upgrading
Coal is mixed with quick lime into mixing tank 5, and mixed material is fitted into the elevated bunker of system for producing calcium carbide, is reloaded into
Furnace of calcium carbide 6 produces calcium carbide.The calcium carbide cooling crush produced, by the size controlling of calcium carbide between 50~80mm, into acetylene
Reaction obtains acetylene in generator 7.
By the system, in 1000kg low-order coal and 2000kg lime stones can obtain 348kg acetylene, 88kg hydrogen,
234kg methane, 800kg carbon dioxide and 395kg carbon monoxide.Acetylene, hydrogen, methane, carbon dioxide and the 38kg of gained
Carbon monoxide, which is passed through in acetylene aromatic hydrocarbons reactor 8, to be reacted, the internal diameter of acetylene aromatic hydrocarbons reactor 8：Length：Heat furnace superintendent
Degree=1:14:8, residence time of the gaseous mixture in thermal reaction area 810 is 0.6s, and the reaction temperature of thermal reaction area 810 is 900 DEG C,
The residence time of catalytic reaction zone 812 is 0.1s, and catalytic temperature is 350 DEG C.Production obtains 260kg light aromatics and 40kg heavys
Aromatic hydrocarbons.It is passed through flue gas to regenerate acetylene aromatic hydrocarbons reactor 8, regenerative process symbiosis is into hydrogen 2.0kg, for reaction after separation
Process uses.
Embodiment 2
As Figure 1-3, agstone is broken to below 45mm, from 5~45mm particle diameters, through belt-conveying to first Jiao
Stove is fired.Middle low-order coal is crushed to below 25mm, from 5~25mm particle diameters, is pyrolyzed through belt-conveying to the second coke oven.Low order
Coal is 1 with lime stone mass ratio:1, coke oven combustion chamber heating-up temperature is 1000 DEG C.By 12h fire and be pyrolyzed after, upgraded coal with
Quick lime is mixed into mixing tank, and mixed material is fitted into the elevated bunker of system for producing calcium carbide, is reloaded into calcium carbide
Stove produces calcium carbide.The calcium carbide cooling crush produced, by the size controlling of calcium carbide between 50~80mm, into acetylene generator
Middle reaction obtains acetylene.
By the system, in 1000kg low-order coal and 1000kg lime stones can obtain 209kg acetylene, 88kg hydrogen,
234kg methane, 491kg carbon dioxide and 245kg carbon monoxide.Acetylene, hydrogen, methane, carbon dioxide and the whole of gained
Carbon monoxide be passed through in acetylene aromatic hydrocarbons reactor and reacted, the internal diameter of acetylene aromatic hydrocarbons reactor 8：Length：Heating furnace
Length=1:14:8, residence time of the gaseous mixture in thermal reaction area is 0.6s, and thermal reaction area reaction temperature is 1100 DEG C, is being catalyzed
The residence time of reaction zone is 0.1s, and catalytic temperature is 600 DEG C.Production obtains 141kg light aromatics and 47kg heavy arenes.It is logical
Enter flue gas to regenerate acetylene aromatic hydrocarbons reactor, regenerative process symbiosis makes into hydrogen 1.4kg after separation for course of reaction
With.
Embodiment 3
As Figure 1-3, agstone is broken to below 45mm, from 5~45mm particle diameters, through belt-conveying to first Jiao
Stove 3 is fired.Middle low-order coal is crushed to below 25mm, from 5~25mm particle diameters, is pyrolyzed through belt-conveying to the second coke oven 4.It is low
Rank coal is 1 with lime stone mass ratio:2, coke oven combustion chamber heating-up temperature is 1000 DEG C.After 12h is fired and is pyrolyzed, upgraded coal
Mixed with quick lime into mixing tank 5, mixed material is fitted into the elevated bunker of system for producing calcium carbide, is reloaded into electricity
Stone stove 6 produces calcium carbide.The calcium carbide cooling crush produced, by the size controlling of calcium carbide between 50~80mm, sent out into acetylene
Reaction obtains acetylene in raw device 7.
By the system, in 1000kg low-order coal and 2000kg lime stones can obtain 348kg acetylene, 88kg hydrogen,
234kg methane, 800kg carbon dioxide and 395kg carbon monoxide.Acetylene, hydrogen, methane, carbon dioxide and the 187kg of gained
Carbon monoxide, which is passed through in acetylene aromatic hydrocarbons reactor 8, to be reacted, the internal diameter of acetylene aromatic hydrocarbons reactor 8：Length：Heat furnace superintendent
Degree=1:14:8, residence time of the gaseous mixture in thermal reaction area 810 is 0.6s, and the reaction temperature of thermal reaction area 810 is 850 DEG C,
The residence time of catalytic reaction zone 812 is 0.1s, and catalytic temperature is 350 DEG C.Production obtains 254kg light aromatics and 35kg heavys
Aromatic hydrocarbons.It is passed through flue gas to regenerate acetylene aromatic hydrocarbons reactor 8, regenerative process symbiosis is into hydrogen 1.9kg, for reaction after separation
Process uses.
Preferred embodiment of the present utility model is these are only, is not used for limiting practical range of the present utility model；If
Spirit and scope of the present utility model are not departed from, the utility model are modified or equivalent substitution, all should be covered in this reality
Among new scope of the claims.
Claims (5)
1. a kind of system that aromatic hydrocarbons is prepared by coal with flue gas reuse function, it is characterised in that include：
Material pretreatment system, there are multiple entrance and exits, for coal and lime stone to be pyrolyzed and fired respectively, obtain
First gas and the first solid, and second gas and the second solid,
Cleaning system, including the first cleaning system, first cleaning system have first gas material inlet and multiple outlets,
For the first gas material purification separation to be obtained into hydrogen, methane, carbon monoxide and light hydrocarbon gas；
Furnace of calcium carbide, the furnace of calcium carbide have the first import, first outlet and CO gas outlet, the furnace of calcium carbide it is described
First import is used to be sent into first solid and the second solid；The CO gas of the furnace of calcium carbide is exported for arranging
Go out carbon monoxide；
Acetylene generator, the acetylene generator have the second import and a second outlet, and described the second of the acetylene generator
Import is connected with the first outlet of the furnace of calcium carbide；The second outlet of the acetylene generator, which is used to discharge, contains acetylene
Gas；
Acetylene aromatic hydrocarbons reactor, the acetylene aromatic hydrocarbons reactor have feeding line, gas distributor, react sleeve pipe, add
Hot stove and discharging pipeline；The feeding line is provided with entrance and exit, and the entrance is used to be passed through from the cleaning system point
The hydrogen and methane that separate out, from the carbon monoxide of furnace of calcium carbide discharge and from acetylene made from the acetylene generator；Institute
State gas distributor be arranged on it is described reaction sleeve pipe inside and positioned at it is described reaction sleeve pipe upper end and with the feed pipe
The outlet of line；Filling ceramic honeycomb body in the reaction sleeve pipe；The reaction sleeve pipe runs through the heating furnace, the heating
The middle part of sleeve pipe is reacted described in stove face；The discharging pipeline connects with the lower end of the reaction sleeve pipe.
2. system according to claim 1, it is characterised in that the material pretreatment system includes：First coke oven and
Two coke ovens, first coke oven are used to be pyrolyzed coal, and second coke oven is used to be fired lime stone；Described first
There is coke oven first material import, the first solid outlet and first gas outlet, second coke oven there is second material to enter
Mouth, the second solid outlet and second gas outlet；First coke oven and second coke oven are combustion chamber shared, the burning
Room has fuel gas inlet and exhanst gas outlet.
3. system according to claim 2, it is characterised in that the CO gas exit of the furnace of calcium carbide is set
Flow divider is put, the flow divider has the first diffluence pass and the second diffluence pass, for the CO gas to be divided into two-way,
Wherein all the way with the entrance of the feeding line of the acetylene aromatic hydrocarbons reactor can breakaway-element be connected, in addition all the way with the burning
The fuel gas inlet of room is connected.
4. system according to claim 2, it is characterised in that the exhanst gas outlet of the combustion chamber and the acetylene aromatic hydrocarbons
The entrance of the feeding line of reactor can breakaway-element connection.
5. system according to claim 2, it is characterised in that the cleaning system also includes the second cleaning system, described
Second cleaning system is connected for purifying the second gas with the second gas outlet of second coke oven, has second gas
Entrance and carbon dioxide outlet.
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